CN111495106A - Temperature control system and temperature control method for active coke adsorption tower - Google Patents
Temperature control system and temperature control method for active coke adsorption tower Download PDFInfo
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- CN111495106A CN111495106A CN201910092115.0A CN201910092115A CN111495106A CN 111495106 A CN111495106 A CN 111495106A CN 201910092115 A CN201910092115 A CN 201910092115A CN 111495106 A CN111495106 A CN 111495106A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0438—Cooling or heating systems
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
Abstract
The invention belongs to the field of chemical industry, and particularly discloses an active coke adsorption tower temperature control system and a temperature control method, wherein the active coke adsorption tower temperature control system comprises: an active coke adsorption tower, a purified flue gas cooler and a chimney; an inlet air chamber, an outlet air chamber, a first-stage adsorption bed layer, a second-stage adsorption bed layer and an interstage air chamber are sequentially arranged in the active coke adsorption tower from bottom to top; the inlet air chamber is connected with a flue gas feeding pipeline to be purified, the outlet air chamber is connected with a purified flue gas discharging pipeline, the purified flue gas discharging pipeline is divided into two branches, the first branch pipeline is connected with the chimney, the second branch pipeline is connected with the inlet of the purified flue gas cooler, and the outlet of the purified flue gas cooler is respectively connected with the interstage air chamber and the inlet air chamber. The purified flue gas is circulated back into the active coke adsorption tower, so that the flue gas temperature at the inlet of the active coke adsorption tower and the temperature rise of a bed layer of the adsorption tower are effectively controlled, the oxygen content and the water content of the flue gas are kept basically unchanged, and the safe and stable operation of the active coke adsorption tower is ensured.
Description
Technical Field
The invention belongs to the field of chemical industry, and particularly relates to a temperature control system and a temperature control method for an active coke adsorption tower.
Background
The active coke dry purification technology starts to be industrially applied in the 80 th of the 20 th century, and has the outstanding advantages of high desulfurization efficiency, no water consumption in reaction, no waste water and residue discharge, no equipment corrosion problem and the like. With the increasing environmental protection requirement, the technology draws more and more attention and is increasingly widely applied. The active coke-drying purification technology is applied to the catalytic cracking device, SO that SO in the regenerated flue gas can be effectively removed2/SO3Simultaneously to NOxParticulate matter and VOCs etc. also have the effect of desorption in coordination, combine upstream SCR and low reaches sack cleaner, whole clean system can purify regeneration flue gas to satisfying the standard requirement.
The active coke adsorption desulfurization is mainly based on chemical adsorption, and the process is a strong exothermic reaction. The reaction heat released in normal operation is absorbed by the flue gas and the active coke, so that the temperature of the flue gas and the temperature of the bed layer are increased to a certain extent. Along with SO in the flue gas2The concentration is continuously increased, and the heat released in the adsorption process is increased, so that the temperature of the flue gas and the temperature of the bed layer are continuously increased, and finally, the active coke bed layer can be over-heated or spontaneously combusted. SO in flue gas treated by the prior active coke dry method flue gas purification process2The concentration usually cannot exceed 5000mg/Nm3But in individual cases SO in flue gases2The concentration can reach 10000mg/Nm3. In addition, the higher the flue gas temperature is, the greater the oxidation exothermic temperature rise of the active coke adsorption bed layer is, so the temperature of the flue gas at the inlet of the active coke adsorption tower is generally required to be controlled.
Catalytic cracking is an important heavy oil lightening process, is a main means for obtaining benefits of refineries, and has the core of a reaction regeneration system. Heavy oil is cracked by the reaction system under the action of catalyst to produce light oilAnd liquefied gases, etc., with a small portion of coke deposited on the catalyst. The regeneration system burns the catalyst deposited with coke at high temperature and in an aerobic environment to realize the regeneration of the catalyst. The regenerated catalyst is sent back to the reaction system, and the catalyst is recycled between the reaction regeneration systems. Because the sulfur content of the raw material processed by the catalytic cracking unit is usually 0.5-1 wt%, SO in the regenerated flue gas is ensured2The content is often less than 2000mg/Nm3In a few cases, 3000mg/Nm3. Since most of the heavy metals in heavy oils, such as Ni, V, etc., are deposited on the catalyst, Ni content is typically up to 11000ppmw and V content is up to 7000 ppmw. V is often V in the regenerator2O5Form exists, as is well known, V2O5Is SO2To SO3Converted catalyst, higher V content on catalyst resulting in SO in regeneration flue gas2/SO3The proportion of the SO in the flue gas of the coal-fired boiler reaches 10 percent or even higher2/SO3The ratio (usually 1% to 2%) is much higher. In addition, the denitration of the regenerated flue gas of the catalytic cracking unit usually adopts a medium-temperature SCR (320-400 ℃), and the active component of the SCR is mainly V2O51% -2% SO is generated after the regeneration flue gas passes through SCR2Conversion to SO3Resulting in SO in the regeneration flue gas3The content is higher. Also, NH due to SCR3The escape rate is 2-3 mg/Nm3Two problems arise: one is NH3With SO3Reaction to form highly viscous NH4HSO4Can adhere to catalyst fine powder in the flue gas, lead to rapid salt formation and blockage of an economizer, and NH4HSO4The generation temperature of (A) is generally 190-240 ℃; second, higher SO3The content causes the problems of higher acid dew point of the flue gas, corrosion to downstream equipment and the like. The two problems seriously affect the long-period stable operation of the catalytic cracking device, and in order to prevent salt deposition blockage and dew point corrosion, the common method is to increase the temperature of the flue gas at the outlet of the economizer, at present, the temperature at the outlet of the economizer of the waste heat boiler of the catalytic device of the petrochemical enterprise is 180-200 ℃, and in one operation period (continuous operation for 3-4 years), because the heat exchange tubes at the coal-saving section gradually deposit salt and deposit ash, the coal-saving section can save the salt and deposit ashThe coal outlet temperature may rise further, and some devices may reach 240-250 ℃ at the end of an operating cycle, and individual devices may reach 280 ℃.
The sulfur recovery device is an important environment-friendly device in petrochemical industry, and usually adopts a Claus process to recover sulfur resources in acid gas. The traditional sulfur device adopts the process of treating the Claus sulfur production and the hydrogenation reduction absorption tail gas to recover sulfur resources, the recovery rate of the sulfur resources of the Claus sulfur production is about 95 percent, and the recovery rate of the sulfur resources of the hydrogenation reduction absorption tail gas treatment is about 5 percent. Wherein the hydrogenation reduction absorption tail gas treatment mainly comprises tail gas hydrogenation, tail gas water washing and cooling (including discharged acidic water stripping), and tail gas MDEA dehydrogenation2S (including MDEA regeneration), tail gas incineration and other units to realize high sulfur resource recovery rate (usually up to more than 99.5%), and a small amount of unrecovered sulfur after treatment enters the tail gas incinerator along with the tail gas to incinerate H2Conversion of S to SO2Followed by tail gas emission (can meet SO in tail gas)2The content is less than 400mg/Nm3). The process is mature, but the process is long, and the investment and operation cost is high. At present, with the rapid development of related desulfurization technologies, the sulfur recovery device has the tendency of canceling the tail gas treatment part of hydrogenation reduction absorption, and tail gas after the sulfur preparation by Claus directly enters a tail gas incinerator to ensure that H in the tail gas incinerator2S, S etc. are all converted to SO2SO in tail gas after incineration2The concentration of the active carbon reaches 10000-30000 mg/Nm3Corresponding, SO3The concentration is 100-1000 mg/Nm3The dew point temperature is relatively high, and the exhaust gas temperature is usually 200-260 ℃.
By comprehensively considering the desulfurization and denitrification effects of the active coke, the simultaneous removal of multiple pollutants, the safe operation in the active coke bed layer and other factors, the ideal desulfurization and denitrification temperature of the active coke is 130-160 ℃, the inlet temperature of the active coke adsorption tower is generally required to be not more than 180 ℃, and the temperature of the active coke bed layer is required to be less than 200 ℃. Therefore, when the active coke-drying purification technology is applied to the regeneration flue gas of a catalytic cracking unit or the tail gas of a sulfur unit, two temperatures need to be solved: firstly, stably controlling the temperature of flue gas at the inlet of an active coke adsorption tower to be not more than 180 ℃; secondly, controlling the temperature rise of the active coke bed layer to be not more than 20 ℃, and controlling the temperature of the active coke bed layer to be less than 200 ℃.
The common measures for cooling the flue gas include the following measures: the smoke gas heat extractor is arranged, the water is sprayed for cooling, the cold air is mixed for cooling, and the like, and the cooling measures can be combined to reduce the temperature of the smoke gas. Wherein, a flue gas heat collector is arranged for SO3In higher concentration and in the presence of small amounts of NH3And when the flue gas of the particulate matter is directly cooled, problems of dew point corrosion, salt deposition, dust deposition and the like can occur; the water spray cooling may cause the water spray not to be completely gasified, SO SO may be dissolved in the fog drops3The problem of corrosion of a flue and downstream equipment is solved, water consumption is increased, the water content in the flue gas is further increased, and the denitration performance of the active coke can be influenced; the cooling of the mixed cold air can greatly increase the oxygen content of the flue gas, so that the oxygen content in the flue gas is higher than the reference oxygen content, the requirement on downstream active coke dry purification facilities is higher, the concentration of pollutants in the flue gas can be directly diluted by the mixed air in the flue gas, and similar measures for directly mixing the air into the flue gas can be gradually limited in future along with the continuous improvement of environmental protection standards.
The two measures are mainly adopted for controlling the temperature rise of the bed layer of the active coke adsorption tower, and the measures are used for reducing SO in the flue gas to be purified2But this measure limits the active coke dry cleaning process to deal with high SO2The application at the time of concentration of the gas; and secondly, the temperature of the flue gas to be purified is reduced, and the heat release of oxidation of the active coke bed is reduced so as to control the temperature rise of the bed.
Disclosure of Invention
The invention aims to provide an active coke adsorption tower temperature control system and a temperature control method which can safely and effectively control the flue gas temperature at the inlet of an active coke adsorption tower and the temperature rise of an adsorption tower bed layer, simultaneously keep the oxygen content and the water content of the flue gas unchanged basically and ensure the safe and stable operation of the active coke adsorption tower.
In order to achieve the above object, in one aspect, the present invention provides an active coke adsorption tower temperature control system, including: an active coke adsorption tower, a purified flue gas cooler and a chimney;
wherein the top of the active coke adsorption tower is provided with an active coke inlet, the bottom of the active coke adsorption tower is provided with an active coke outlet,
an inlet air chamber, an outlet air chamber, a first-stage adsorption bed layer and a second-stage adsorption bed layer which are respectively positioned on the side surfaces of the inlet air chamber and the outlet air chamber, and an interstage air chamber which is positioned on the side surfaces of the first-stage adsorption bed layer and the second-stage adsorption bed layer are sequentially arranged in the active coke adsorption tower from bottom to top;
the inlet air chamber is connected with a to-be-purified flue gas feeding pipeline, the outlet air chamber is connected with a purified flue gas discharging pipeline, the purified flue gas discharging pipeline is divided into two branches, a first branch pipeline is connected with the chimney, a second branch pipeline is connected with an inlet of the purified flue gas cooler, and an outlet of the purified flue gas cooler is respectively connected with the interstage air chamber and the inlet air chamber.
In the invention, the active coke adsorption tower adopts a two-stage cross-flow adsorption bed structure, wherein the first-stage adsorption bed layer is arranged at the lower layer, the second-stage adsorption bed layer is arranged at the upper layer, and the flue gas to be purified and the active coke bed layer are in cross-flow contact, wherein the first-stage adsorption bed layer and the second-stage adsorption bed layer are arranged on the side surfaces of the inlet air chamber and the outlet air chamber, the interstage air chambers are arranged on the side surfaces of the first-stage adsorption bed layer and the second-stage adsorption bed layer, and when the flow rate of3In the case of the reaction, the active coke adsorption tower preferably adopts a structure of two adsorption beds, namely a first-stage adsorption bed and a second-stage adsorption bed are respectively arranged at the peripheries of an inlet air chamber and an outlet air chamber, and an interstage air chamber is arranged at the peripheries of the first-stage adsorption bed and the second-stage adsorption bed and can be selected as a sleeve structure; when the flow rate of the flue gas to be purified is less than 30000Nm3In the case of the/h, the active coke adsorption tower preferably adopts a single adsorption bed layer structure, namely the inlet air chamber and the outlet air chamber are arranged on one side of the first-stage adsorption bed layer and one side of the second-stage adsorption bed layer, and the interstage air chamber is arranged on the other side of the first-stage adsorption bed layer and the second-stage adsorption bed layer and can be in a structure that the air chamber, the adsorption bed layers and the interstage air chamber are arranged in a straight line.
The flue gas to be purified is discharged from an outlet air chamber through the first-stage adsorption bed layer and the second-stage adsorption bed layer, then a part of the flue gas is led out to be divided into two branches, the first branch returns to an inlet air chamber of the adsorption tower to be mixed with the flue gas to be purified so as to control the temperature required by desulfurization and denitration in the first-stage adsorption bed layer, and the second branch returns to an air chamber between active coke adsorption tower stages so as to adjust the temperature of the flue gas in the air chamber, control the temperature of the flue gas entering the second-stage adsorption bed layer in the active coke adsorption tower, and ensure the safe and stable operation of the.
The invention adopts the purified flue gas to circulate in the active coke adsorption tower, because SO in the purified flue gas3And NH3The content is extremely low, the pollutant concentration is very low, and the problems of salt deposition, dust deposition and dew point corrosion of the clean flue gas cooler can not occur. The type of the clean smoke cooler has no special requirement, air cooling or circulating water cooling can be adopted, and the material of the clean smoke cooler is preferably a non-metallic heat exchange tube, and particularly fluoroplastics and the like can be selected.
According to the content of the particles in the flue gas to be purified and the requirement of the particles in the purified flue gas, the temperature control system of the active coke adsorption tower can further comprise a first dust remover, wherein the inlet of the first dust remover is connected with a flue gas feeding pipeline to be purified, and the outlet of the first dust remover is connected with an inlet gas chamber. The type of the first dust remover is not particularly limited, and the first dust remover can be any one of an electric dust remover, a bag-type dust remover and an electric bag dust remover.
When the inlet of the active coke adsorption tower is provided with the first dust remover, the cooled first clean flue gas can be connected to the inlet flue of the first dust remover to control the operation temperature of the first dust remover, and can also be connected to the inlet flue of the active coke adsorption tower, and is preferentially connected to the inlet flue of the active coke adsorption tower; when the first dust remover is not arranged at the inlet of the active coke adsorption tower, the cooled first clean flue gas is connected to the inlet flue of the active coke adsorption tower.
According to the invention, according to the content of the particulate matters in the flue gas to be purified and the requirement of the particulate matters in the purified flue gas, the temperature control system of the active coke adsorption tower can further comprise a second dust remover and/or an induced draft fan, wherein the second dust remover and/or the induced draft fan are/is arranged on a connecting pipeline of the outlet air chamber and the chimney. The purified flue gas flow for reflux cooling can be judged to be led out from the inlet of the second dust remover or led out from the outlet of the second dust remover according to the content of particulate matters in the flue gas.
According to the invention, preferably, when the active coke adsorption tower temperature control system only comprises a second dust remover, the inlet of the second dust remover is connected with the outlet gas chamber, the outlet of the second dust remover is connected with the chimney, and the inlet of the purified flue gas cooler is connected with the inlet or the outlet of the second dust remover;
when the temperature control system of the active coke adsorption tower only comprises an induced draft fan, the inlet of the induced draft fan is connected with the outlet air chamber, the outlet of the induced draft fan is connected with the chimney, and the inlet of the purified flue gas cooler is connected with the outlet of the induced draft fan;
when the temperature control system of the active coke adsorption tower comprises a second dust remover and an induced draft fan, the outlet air chamber is sequentially connected with the second dust remover, the induced draft fan and a chimney, the inlet of the purified flue gas cooler is connected with the inlet of the second dust remover, the outlet of the second dust remover or the outlet of the induced draft fan, or the outlet air chamber is sequentially connected with an induced draft fan, a second dust remover and a chimney, the inlet of the clean flue gas cooler is connected with the outlet of the induced draft fan or the outlet of the second dust remover, further preferably, the induced draft fan is arranged at the upstream of the second dust remover, namely, the outlet air chamber is sequentially connected with the induced draft fan, the second dust remover and the chimney, the flow direction of the flue gas is the active coke adsorption tower → the induced draft fan → the second dust remover → the chimney, the purified flue gas discharged from the outlet air chamber is preferentially led out from the outlet of the induced draft fan and the inlet of the second dust remover, and the purified flue gas can also be led out from the outlet of the second dust remover and sent to the purified flue gas cooler.
According to the invention, preferably, the active coke adsorption tower temperature control system further comprises a booster fan, and the booster fan is arranged on the second branch pipeline.
In the present invention, in order to prevent SO in the pipeline3Dew point corrosion, which can upgrade part of flue materials to nickel-based alloy or nonmetal; meanwhile, in order to prevent the temperature of the flue gas to be purified from suddenly rising greatly, an emergency water spraying cooling device can be arranged at the upstream position of the first dust remover.
The invention also provides a temperature control method of the active coke adsorption tower, which is carried out in the temperature control system of the active coke adsorption tower, and comprises the following steps:
the active coke enters the tower from an active coke inlet at the top of the active coke adsorption tower, sequentially passes through the second-stage adsorption bed layer and the first-stage adsorption bed layer from top to bottom and is sent out from an active coke outlet at the bottom of the tower;
the flue gas to be purified enters an inlet gas chamber of the active coke adsorption tower through a flue gas feeding pipeline to be purified, and is in cross flow contact with active coke in a first-stage adsorption bed layer to perform first-stage adsorption purification, the flue gas which completes the first-stage adsorption purification is subjected to gas redistribution through an interstage gas chamber and then ascends to enter a second-stage adsorption bed layer to be in cross flow contact with the active coke to perform second-stage adsorption purification, the flue gas which completes the second-stage adsorption purification leaves the active coke adsorption tower from an outlet gas chamber, one part of the purified flue gas which leaves the active coke adsorption tower is sent to a chimney, and the other part of the purified flue gas is sent to the flue gas feeding pipeline to be purified and/or the.
The range of the flue gas to be purified which is suitable for the invention is wide, and the flue gas can be regenerated flue gas of a catalytic cracking device, or gas which has similar properties and can cause salt deposition, dust deposition and acid dew point corrosion by directly adopting a flue gas cooler for cooling; the flue gas to be purified can also be high SO2And SO3Sulfur plant tail gas of similar character, direct cooling with flue gas coolers can lead to acid dew point corrosion and high SO content2The content results in gas with excessively high temperature of the active coke adsorption tower.
When treating the regeneration flue gas of a catalytic cracking unit, due to its SO2Low content of SO3/SO2The high-temperature regenerated flue gas contains fine particles, and the temperature of the regenerated flue gas can be continuously increased due to gradual salt deposition and ash deposition of the heat exchange tube of the coal-saving section in an operation period of the coal-saving section outlet of the upstream catalytic cracking waste heat boiler. In the invention, the purified flue gas is cooled and then returns to the inlet air chamber of the active coke adsorption tower to be mixed with the flue gas to be purified, so that the following key problems can be solved: firstly, the inlet of the active coke adsorption tower is reducedSO in the flue gas to be purified3Content, correspondingly lowering the acid dew point temperature; and secondly, controlling the temperature of the flue gas to be purified at the inlet of the adsorption tower to be the temperature required by the desulfurization and denitrification of the active coke under the condition that the temperature of the outlet of the coal saving section of the upstream waste heat boiler is continuously increased.
For treating tail gas of sulfur plant, due to SO2The concentration is as high as 10000-30000 mg/Nm3，SO3The concentration is 100-1000 mg/Nm3In the invention, the purified flue gas is cooled and then respectively returned to an inlet gas chamber and an interstage gas chamber of the active coke adsorption tower, and the feed temperature of the active coke adsorption tower and the flue gas temperature of the interstage gas chamber are respectively controlled, so as to solve the following key problems: firstly, the SO in the flue gas to be purified at the inlet of the active coke adsorption tower is reduced3Content, correspondingly lowering the acid dew point temperature; secondly, controlling the temperature of the flue gas to be purified at the inlet of the adsorption tower at the temperature required by the desulfurization and denitrification of the active coke; thirdly, reducing SO in flue gas at the inlet of the active coke adsorption tower2The content is controlled to control the temperature rise of the first-stage adsorption bed layer; fourthly, reducing the temperature of the interstage flue gas, and further reducing the SO at the inlet of the second-stage adsorption bed2In order to ensure SO of the second-stage adsorption bed layer2Purifying effect, and controlling the temperature rise of the second adsorption bed layer.
The purified flue gas is circulated back to the active coke adsorption tower, one part of the purified flue gas is mixed with the flue gas to be purified and then enters the active coke adsorption tower from the inlet air chamber, the temperature rise in the first-stage adsorption bed is preferably controlled not to exceed 20 ℃, the other part of the purified flue gas is mixed with the flue gas after the first-stage adsorption purification in the interstage air chamber, and the temperature rise in the second-stage adsorption bed is preferably controlled not to exceed 20 ℃. Because the purified flue gas is returned to the active coke adsorption tower, the oxygen content and the water content in the tower can be kept unchanged, and the safe and stable operation of the active coke adsorption tower is ensured.
According to the invention, preferably, the temperature of the flue gas to be purified is 160-.
According to the invention, preferably the mass ratio of the flue gas to be purified to the purified flue gas fed to the flue gas feed line to be purified is between 0 and 3, more preferably between 0.2 and 2; the mass ratio of the purified flue gas sent to the interstage air chamber to the flue gas at the outlet of the first-stage adsorption bed layer is 0-2, and the further optimization is 0.1-1.5
Compared with the prior art, the invention has the following advantages:
1. the invention returns the partially purified flue gas to the inlet gas chamber, thereby reducing SO3With SO2The content, correspondingly reducing the acid dew point temperature, and controlling the temperature rise of the first-stage adsorption bed layer; because the purified flue gas is mixed with the flue gas to be purified, the SO in the flue gas to be purified is reduced2/SO3/NOxThe content of the active coke ensures the pollutant removal effect of the active coke adsorption tower.
2. The invention returns the flue gas after partial purification to the interstage air chamber, controls the temperature rise of the second-stage adsorption bed layer by reducing the oxidation heat release of the second-stage adsorption bed layer, and can further improve the SO of the second-stage adsorption bed layer because the low temperature is favorable for the desulfurization of the active coke2Removal rate, SO2The content reduction also reduces the temperature rise of the second-stage adsorption bed layer.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout.
FIG. 1 shows a schematic diagram of the temperature control system of the active coke adsorption tower in example 1 of the present invention.
FIG. 2 shows a schematic diagram of the temperature control system of the activated coke adsorption tower in example 2 of the present invention.
FIG. 3 shows a schematic diagram of the temperature control system of the activated coke adsorption tower in example 3 of the present invention.
FIG. 4 shows a schematic diagram of the temperature control system of the activated coke adsorption tower in example 4 of the present invention.
FIG. 5 shows a schematic diagram of the temperature control system of the activated coke adsorption tower of example 5 of the present invention.
FIG. 6 shows a schematic diagram of the temperature control system of the activated coke adsorption tower of example 6 of the present invention.
Description of the reference numerals
A. A first dust remover; B. an activated coke adsorption tower; b1, inlet plenum; b2, a first-stage adsorption bed layer; b3, an interstage gas chamber; b4, a second-stage adsorption bed layer; b5, an outlet air chamber; C. an induced draft fan; D. a clean flue gas cooler; E. a second dust remover; F. a chimney; G. a booster fan;
1. the flue gas to be purified; 2. flue gas at the outlet of the first dust remover; 3. the inlet of the adsorption tower is used for purifying smoke; 4. purifying flue gas at an outlet of the adsorption tower; 5. purifying flue gas at an outlet of the induced draft fan; 6. the inlet of the second dust remover is used for cleaning flue gas; 7. the purified flue gas is refluxed; 8. purifying the flue gas in a cooler; 9. cooling the first clean flue gas; 10. cooling the second clean flue gas; 11. purifying flue gas from a chimney; 12. ammonia; 13. regenerating coke; 14. coke generation is to be carried out; 15. and (5) injecting water.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein.
Example 1
Flue gas treatment is carried out by adopting an active coke adsorption tower temperature control system as shown in figure 1.
This active burnt adsorption tower temperature control system includes: the system comprises an active coke adsorption tower B, a clean flue gas cooler D, a chimney F, a first dust remover A and a booster fan G;
wherein the top of the active coke adsorption tower B is provided with an active coke inlet, the bottom of the active coke adsorption tower B is provided with an active coke outlet,
the active coke adsorption tower B adopts two adsorption bed layer structures, and an inlet air chamber B1, an outlet air chamber B5, a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 which are respectively positioned at the outer sides of an inlet air chamber B1 and an outlet air chamber B5, and an interstage air chamber B3 which is positioned at the outer sides of a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 are sequentially arranged in the tower from bottom to top;
the inlet of the first deduster A is connected with a flue gas feeding pipeline to be purified, the outlet of the first deduster A is connected with an inlet air chamber B1, an outlet air chamber B5 is connected with a clean flue gas discharging pipeline, the clean flue gas discharging pipeline is divided into two branches, a first branch pipeline is connected with a chimney F, a second branch pipeline is sequentially connected with a booster fan G and the inlet of a clean flue gas cooler D, and the outlet of the clean flue gas cooler D is respectively connected with an interstage air chamber B3 and an inlet air chamber B1.
The temperature control method of the active coke adsorption tower comprises the following steps:
the flue gas 1 to be purified from the upstream at 180 ℃ enters a first dust remover A to reduce the content of particulate matters to 50mg/Nm3Then, the flue gas is mixed with first clean flue gas 9 to reduce the temperature of the feed flue gas to 140 ℃, then enters a first adsorption bed layer B2 through an inlet gas chamber B1, is in cross-flow contact with active coke in a first adsorption bed layer B2 to carry out primary adsorption purification for removing pollutants such as desulfurization, dust removal and the like, the flue gas which completes the primary adsorption purification is subjected to gas redistribution through an interstage gas chamber B3 and then ascends to enter a second adsorption bed layer B4, wherein the temperature of the flue gas which completes the primary adsorption purification is increased to 160 ℃, the flue gas enters an interstage gas chamber B3 to be mixed with second clean flue gas 10 and then is cooled to 150 ℃, and then the flue gas is mixed with injected ammonia 12 and then enters a second adsorption bed layer B4 to complete the removal of NO in the flue gasxAnd the rest of SO2The second-stage adsorption purification is carried out, then the second-stage adsorption purification is discharged out of the active coke adsorption tower B through an outlet gas chamber B5, one part of the purified flue gas leaving the active coke adsorption tower B is sent to a chimney F, the other part of the purified flue gas enters a purified flue gas cooler D after being pressurized by a booster fan G to obtain a first purified flue gas 9 and a second purified flue gas 10 after being cooled, the first purified flue gas 9 returns to an inlet gas chamber B1 of the active coke adsorption tower to be mixed with the outlet flue gas 2 of the first dust remover, and the second purified flue gas 10 returns to an inter-stage gas chamber B3 of the active coke adsorption tower.
The regenerated coke 13 enters the active coke adsorption tower B from the top of the tower, sequentially passes through a second-stage adsorption bed layer B4 and a first-stage adsorption bed layer B2 under the action of gravity, and is discharged from the bottom of the tower as coke to be regenerated and sent to regeneration.
Example 2
Flue gas treatment is carried out by adopting an active coke adsorption tower temperature control system as shown in figure 2.
This active burnt adsorption tower temperature control system includes: the system comprises an active coke adsorption tower B, a clean flue gas cooler D, a chimney F, a first dust remover A and a draught fan C;
wherein the top of the active coke adsorption tower B is provided with an active coke inlet, the bottom of the active coke adsorption tower B is provided with an active coke outlet,
the active coke adsorption tower B adopts two adsorption bed layer structures, and an inlet air chamber B1, an outlet air chamber B5, a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 which are respectively positioned at the outer sides of an inlet air chamber B1 and an outlet air chamber B5, and an interstage air chamber B3 which is positioned at the outer sides of a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 are sequentially arranged in the tower from bottom to top;
the inlet of the first deduster A is connected with a flue gas feeding pipeline to be purified, the outlet of the first deduster A is connected with an inlet air chamber B1, an outlet air chamber B5 is connected with an induced draft fan C, the outlet of the induced draft fan C is divided into two branches, a first branch pipeline is connected with a chimney F, a second branch pipeline is connected with the inlet of a purified flue gas cooler D, and the outlet of the purified flue gas cooler D is respectively connected with an interstage air chamber B3 and an inlet air chamber B1.
The temperature control method of the active coke adsorption tower comprises the following steps:
the flue gas 1 to be purified from the upstream at 210 ℃ enters a first dust remover A to reduce the content of particulate matters to 50mg/Nm3Then, the flue gas is mixed with first clean flue gas 9 to reduce the temperature of the feed flue gas to 160 ℃, then enters a first adsorption bed layer B2 through an inlet gas chamber B1, is in cross-flow contact with active coke in a first adsorption bed layer B2 to carry out primary adsorption purification for removing pollutants such as desulfurization, dust removal and the like, the flue gas which completes the primary adsorption purification is subjected to gas redistribution through an interstage gas chamber B3 and then ascends to enter a second adsorption bed layer B4, wherein the temperature of the flue gas which completes the primary adsorption purification is increased to 180 ℃, the flue gas enters an interstage gas chamber B3 to be mixed with second clean flue gas 10 and then is cooled to 170 ℃, and then the flue gas is mixed with injected ammonia 12 and then enters a second adsorption bed layer B4 to complete the removal of NO in the flue gasxAnd the rest of SO2Then the second-stage adsorption purification is carried out, and the gas is discharged out of the active coke adsorption tower B through an outlet gas chamber B5 and leaves the active coke adsorption towerAnd B, conveying the purified flue gas to an induced draft fan C, conveying one part of the purified flue gas discharged from an outlet of the induced draft fan to a chimney F, conveying the other part of the purified flue gas into a purified flue gas cooler D to obtain a cooled first purified flue gas 9 and a cooled second purified flue gas 10, returning the first purified flue gas 9 to an inlet gas chamber B1 of the active coke adsorption tower to be mixed with the outlet flue gas 2 of the first dust remover, and returning the second purified flue gas 10 to an inter-stage gas chamber B3 of the active coke adsorption tower.
The regenerated coke 13 enters the active coke adsorption tower B from the top of the tower, sequentially passes through a second-stage adsorption bed layer B4 and a first-stage adsorption bed layer B2 under the action of gravity, and is discharged from the bottom of the tower as coke to be regenerated and sent to regeneration.
Example 3
Flue gas treatment was carried out using an active coke adsorption tower temperature control system as shown in figure 3.
This active burnt adsorption tower temperature control system includes: the system comprises an active coke adsorption tower B, a clean flue gas cooler D, a chimney F, a first dust remover A, a booster fan G and a second dust remover E;
wherein the top of the active coke adsorption tower B is provided with an active coke inlet, the bottom of the active coke adsorption tower B is provided with an active coke outlet,
the active coke adsorption tower B adopts two adsorption bed layer structures, and an inlet air chamber B1, an outlet air chamber B5, a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 which are respectively positioned at the outer sides of an inlet air chamber B1 and an outlet air chamber B5, and an interstage air chamber B3 which is positioned at the outer sides of a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 are sequentially arranged in the tower from bottom to top;
the inlet of the first deduster A is connected with a flue gas feeding pipeline to be purified, the outlet of the first deduster A is connected with an inlet air chamber B1, an outlet air chamber B5 is connected with a clean flue gas discharging pipeline, the clean flue gas discharging pipeline is divided into two branches, the first branch pipeline is sequentially connected with a second deduster E and a chimney F, the second branch pipeline is sequentially connected with a booster fan G and an inlet of a clean flue gas cooler D, wherein the inlet of the clean flue gas cooler D is connected with the inlet of the second deduster E, and the outlet of the clean flue gas cooler D is respectively connected with an interstage air chamber B3 and an inlet air chamber B1.
The temperature control method of the active coke adsorption tower comprises the following steps:
from upstream, the flue gas 1 to be purified at 250 ℃ enters the first stageThe dust collector A reduces the content of the particulate matters to 50mg/Nm3Then the flue gas is mixed with first clean flue gas 9 to reduce the temperature of the feed flue gas to 180 ℃, then enters a first adsorption bed layer B2 through an inlet gas chamber B1, is in cross-flow contact with active coke in the first adsorption bed layer B2 to carry out primary adsorption purification for removing pollutants such as desulfurization, dust removal and the like, the temperature of the flue gas after the primary adsorption purification is increased to 190 ℃, enters an interstage gas chamber B3 for gas redistribution and then ascends to enter a second adsorption bed layer B4, wherein the flue gas after the primary adsorption purification is mixed with second clean flue gas 10 in an interstage gas chamber B3 and then is cooled to 180 ℃, and then enters a second adsorption bed layer B4 after being mixed with injected ammonia 12 to complete removal of NO in the flue gasxAnd the rest of SO2The second-stage adsorption purification is carried out, then the second-stage adsorption purification is discharged out of the active coke adsorption tower B through an outlet air chamber B5, one part of the purified flue gas leaving the active coke adsorption tower B is dedusted by a second deduster E and then sent to a chimney F, the other part of the purified flue gas is pressurized by a booster fan G and then enters a clean flue gas cooler D to obtain a first clean flue gas 9 and a second clean flue gas 10 after being cooled, the first clean flue gas 9 returns to an inlet air chamber B1 of the active coke adsorption tower to be mixed with the outlet flue gas 2 of the first deduster, and the second clean flue gas 10 returns to an inter-stage air chamber B3 of the active coke.
The regenerated coke 13 enters the active coke adsorption tower B from the top of the tower, sequentially passes through a second-stage adsorption bed layer B4 and a first-stage adsorption bed layer B2 under the action of gravity, and is discharged from the bottom of the tower as coke to be regenerated and sent to regeneration.
Example 4
Flue gas treatment was carried out using an active coke adsorption tower temperature control system as shown in figure 4.
This active burnt adsorption tower temperature control system includes: the system comprises an active coke adsorption tower B, a clean flue gas cooler D, a chimney F, a first dust remover A, a draught fan C and a second dust remover E;
wherein the top of the active coke adsorption tower B is provided with an active coke inlet, the bottom of the active coke adsorption tower B is provided with an active coke outlet,
the active coke adsorption tower B adopts two adsorption bed layer structures, and an inlet air chamber B1, an outlet air chamber B5, a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 which are respectively positioned at the outer sides of an inlet air chamber B1 and an outlet air chamber B5, and an interstage air chamber B3 which is positioned at the outer sides of a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 are sequentially arranged in the tower from bottom to top;
the inlet of the first dust remover A is connected with a flue gas feeding pipeline to be purified, the outlet of the first dust remover A is connected with an inlet air chamber B1, an outlet air chamber B5 is connected with an induced draft fan C, the outlet of the induced draft fan C is divided into two branches, a first branch pipeline is sequentially connected with a second dust remover E and a chimney F, a second branch pipeline is connected with the inlet of a purified flue gas cooler D, and the outlet of the purified flue gas cooler D is respectively connected with an interstage air chamber B3 and an inlet air chamber B1.
The temperature control method of the active coke adsorption tower comprises the following steps:
the flue gas 1 to be purified at 220 ℃ from upstream enters a first dust remover A to reduce the content of particulate matters to 50mg/Nm3Then, the flue gas is mixed with first clean flue gas 9 to reduce the temperature of the feed flue gas to 170 ℃, then enters a first adsorption bed layer B2 through an inlet gas chamber B1, is in cross-flow contact with active coke in a first adsorption bed layer B2 to carry out primary adsorption purification for removing pollutants such as desulfurization, dust removal and the like, the flue gas which completes the primary adsorption purification is subjected to gas redistribution through an interstage gas chamber B3 and then ascends to enter a second adsorption bed layer B4, wherein the temperature of the flue gas which completes the primary adsorption purification is increased to 190 ℃, the flue gas enters an interstage gas chamber B3 to be mixed with second clean flue gas 10 and then is cooled to 180 ℃, and then the flue gas is mixed with injected ammonia 12 and then enters a second adsorption bed layer B4 to complete the removal of NO in the flue gasxAnd the rest of SO2The second-stage adsorption purification is carried out, the second-stage adsorption purification is discharged out of the active coke adsorption tower B through an outlet air chamber B5, purified flue gas leaving the active coke adsorption tower B is sent to an induced draft fan C, one part of the purified flue gas discharged from the outlet of the induced draft fan is dedusted by a second deduster E and then sent to a chimney F, the other part of the purified flue gas enters a purified flue gas cooler D to be cooled into first purified flue gas 9 and second purified flue gas 10, the first purified flue gas 9 returns to an inlet air chamber B1 of the active coke adsorption tower to be mixed with outlet flue gas 2 of the first deduster, and the second purified flue gas 10 returns to an inter-stage air chamber B3 of the active.
The regenerated coke 13 enters the active coke adsorption tower B from the top of the tower, sequentially passes through a second-stage adsorption bed layer B4 and a first-stage adsorption bed layer B2 under the action of gravity, and is discharged from the bottom of the tower as coke to be regenerated and sent to regeneration.
Example 5
Flue gas treatment was carried out using an active coke adsorption tower temperature control system as shown in figure 5.
This active burnt adsorption tower temperature control system includes: the system comprises an active coke adsorption tower B, a clean flue gas cooler D, a chimney F, a first dust remover A, a draught fan C and a second dust remover E;
wherein the top of the active coke adsorption tower B is provided with an active coke inlet, the bottom of the active coke adsorption tower B is provided with an active coke outlet,
the active coke adsorption tower B adopts a single adsorption bed layer structure, and a first-stage adsorption bed layer B2, a second-stage adsorption bed layer B4, an inlet air chamber B1 and an outlet air chamber B5 which are respectively positioned on one sides of the first-stage adsorption bed layer B2 and the second-stage adsorption bed layer B4, and an interstage air chamber B3 which is respectively positioned on the other sides of the first-stage adsorption bed layer B2 and the second-stage adsorption bed layer B4 are sequentially arranged in the tower from bottom to top;
the inlet of the first dust remover A is connected with a flue gas feeding pipeline to be purified, the outlet of the first dust remover A is connected with an inlet air chamber B1, an outlet air chamber B5 is connected with an induced draft fan C, the outlet of the induced draft fan C is divided into two branches, a first branch pipeline is sequentially connected with a second dust remover E and a chimney F, a second branch pipeline is connected with the inlet of a purified flue gas cooler D, and the outlet of the purified flue gas cooler D is respectively connected with an interstage air chamber B3 and an inlet air chamber B1.
The temperature control method of the active coke adsorption tower comprises the following steps:
the flue gas 1 to be purified at 280 ℃ from upstream enters a first dust remover A to reduce the content of particulate matters to 50mg/Nm3Then, the flue gas is mixed with first clean flue gas 9 to reduce the temperature of the feed flue gas to 180 ℃, then enters a first adsorption bed layer B2 through an inlet air chamber B1, is in cross-flow contact with active coke in the first adsorption bed layer B2 to carry out primary adsorption purification for removing pollutants such as desulfurization, dust removal and the like, the flue gas which completes the primary adsorption purification is subjected to gas redistribution through an interstage air chamber B3 and then ascends to enter a second adsorption bed layer B4, wherein the temperature of the flue gas which completes the primary adsorption purification is increased to 190 ℃, the flue gas enters an interstage air chamber B3 to be mixed with second clean flue gas 10 and then is cooled to 180 ℃, and then the flue gas is mixed with injected ammonia 12After being mixed, the mixture enters a second-stage adsorption bed layer B4 to finish the removal of NO in the flue gasxAnd the rest of SO2The second-stage adsorption purification is carried out, the second-stage adsorption purification is discharged out of the active coke adsorption tower B through an outlet air chamber B5, purified flue gas leaving the active coke adsorption tower B is sent to an induced draft fan C, one part of the purified flue gas discharged from the outlet of the induced draft fan is dedusted by a second deduster E and then sent to a chimney F, the other part of the purified flue gas enters a purified flue gas cooler D to be cooled into first purified flue gas 9 and second purified flue gas 10, the first purified flue gas 9 returns to an inlet air chamber B1 of the active coke adsorption tower to be mixed with outlet flue gas 2 of the first deduster, and the second purified flue gas 10 returns to an inter-stage air chamber B3 of the active.
The regenerated coke 13 enters the active coke adsorption tower B from the top of the tower, sequentially passes through a second-stage adsorption bed layer B4 and a first-stage adsorption bed layer B2 under the action of gravity, and is discharged from the bottom of the tower as coke to be regenerated and sent to regeneration.
Example 6
Flue gas treatment was carried out using an active coke adsorption tower temperature control system as shown in figure 6.
This active burnt adsorption tower temperature control system includes: the system comprises an active coke adsorption tower B, a clean flue gas cooler D, a chimney F, a first dust remover A, a draught fan C, a second dust remover E and a booster fan G;
wherein the top of the active coke adsorption tower B is provided with an active coke inlet, the bottom of the active coke adsorption tower B is provided with an active coke outlet,
the active coke adsorption tower B adopts two adsorption bed layer structures, and an inlet air chamber B1, an outlet air chamber B5, a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 which are respectively positioned at the outer sides of an inlet air chamber B1 and an outlet air chamber B5, and an interstage air chamber B3 which is positioned at the outer sides of a first-stage adsorption bed layer B2 and a second-stage adsorption bed layer B4 are sequentially arranged in the tower from bottom to top;
the inlet of the first dust remover A is connected with a flue gas feeding pipeline to be purified, the outlet of the first dust remover A is connected with an inlet air chamber B1, an outlet air chamber B5 is connected with a purified flue gas discharging pipeline, the purified flue gas discharging pipeline is divided into two branches, the first branch pipeline is sequentially connected with a second dust remover E, an induced draft fan C and a chimney F, the second branch pipeline is sequentially connected with an inlet of a booster fan G and an inlet of a purified flue gas cooler D, and the outlet of the purified flue gas cooler D is respectively connected with an interstage air chamber B3 and an inlet air chamber B1.
The temperature control method of the active coke adsorption tower comprises the following steps:
the flue gas 1 to be purified from the upstream at 180 ℃ enters a first dust remover A to reduce the content of particulate matters to 50mg/Nm3Then, the flue gas is mixed with first clean flue gas 9 to reduce the temperature of the feed flue gas to 150 ℃, then enters a first adsorption bed layer B2 through an inlet gas chamber B1, is in cross-flow contact with active coke in a first adsorption bed layer B2 to carry out primary adsorption purification for removing pollutants such as desulfurization, dust removal and the like, the flue gas which completes the primary adsorption purification is subjected to gas redistribution through an interstage gas chamber B3 and then ascends to enter a second adsorption bed layer B4, wherein the temperature of the flue gas which completes the primary adsorption purification is increased to 170 ℃, the flue gas enters an interstage gas chamber B3 to be mixed with second clean flue gas 10 and then is cooled to 160 ℃, and then the flue gas is mixed with injected ammonia 12 and then enters a second adsorption bed layer B4 to complete the removal of NO in the flue gasxAnd the rest of SO2The second-stage adsorption purification is carried out, then the flue gas is discharged out of an active coke adsorption tower B through an outlet gas chamber B5, one part of the purified flue gas leaving the active coke adsorption tower B is dedusted by a second deduster E and then is sent to a chimney F through a draught fan C, the other part of the purified flue gas is pressurized by a booster fan G and then enters a clean flue gas cooler D to obtain a first clean flue gas 9 and a second clean flue gas 10 after being cooled, the first clean flue gas 9 returns to an inlet gas chamber B1 of the active coke adsorption tower to be mixed with the outlet flue gas 2 of the first deduster, and the second clean flue gas 10 returns to an inter-stage gas chamber B3 of the active coke.
The regenerated coke 13 enters the active coke adsorption tower B from the top of the tower, sequentially passes through a second-stage adsorption bed layer B4 and a first-stage adsorption bed layer B2 under the action of gravity, and is discharged from the bottom of the tower as coke to be regenerated and sent to regeneration.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (10)
1. The utility model provides an active burnt adsorption tower temperature control system which characterized in that, this active burnt adsorption tower temperature control system includes: an active coke adsorption tower, a purified flue gas cooler and a chimney;
wherein the top of the active coke adsorption tower is provided with an active coke inlet, the bottom of the active coke adsorption tower is provided with an active coke outlet,
an inlet air chamber, an outlet air chamber, a first-stage adsorption bed layer and a second-stage adsorption bed layer which are respectively positioned on the side surfaces of the inlet air chamber and the outlet air chamber, and an interstage air chamber which is positioned on the side surfaces of the first-stage adsorption bed layer and the second-stage adsorption bed layer are sequentially arranged in the active coke adsorption tower from bottom to top;
the inlet air chamber is connected with a to-be-purified flue gas feeding pipeline, the outlet air chamber is connected with a purified flue gas discharging pipeline, the purified flue gas discharging pipeline is divided into two branches, a first branch pipeline is connected with the chimney, a second branch pipeline is connected with an inlet of the purified flue gas cooler, and an outlet of the purified flue gas cooler is respectively connected with the interstage air chamber and the inlet air chamber.
2. The active coke adsorption tower temperature control system of claim 1, further comprising a first dust collector, wherein an inlet of the first dust collector is connected to the flue gas feed line to be purified, and an outlet of the first dust collector is connected to the inlet plenum.
3. The active coke adsorption tower temperature control system of claim 1, further comprising a second dust collector and/or an induced draft fan, wherein the second dust collector and/or the induced draft fan are/is arranged on a connecting line of the outlet air chamber and the chimney.
4. The active coke adsorption tower temperature control system of claim 3,
when the temperature control system of the active coke adsorption tower only comprises a second dust remover, the inlet of the second dust remover is connected with the outlet gas chamber, the outlet of the second dust remover is connected with the chimney, and the inlet of the purified flue gas cooler is connected with the inlet or the outlet of the second dust remover;
when the temperature control system of the active coke adsorption tower only comprises an induced draft fan, the inlet of the induced draft fan is connected with the outlet air chamber, the outlet of the induced draft fan is connected with the chimney, and the inlet of the purified flue gas cooler is connected with the outlet of the induced draft fan;
when active coke adsorption tower temperature control system includes second dust remover and draught fan, the export air chamber links to each other with second dust remover, draught fan and chimney in proper order, net flue gas cooler entry links to each other with second dust remover entry, second dust remover export or draught fan export, perhaps the export air chamber links to each other with draught fan, second dust remover and chimney in proper order, net flue gas cooler entry links to each other with draught fan export or second dust remover export.
5. The active coke adsorption tower temperature control system of claim 1 wherein the inlet plenum and the outlet plenum are disposed on one side of the first and second adsorbent beds and the interstage plenum is disposed on the other side of the first and second adsorbent beds.
6. The active coke adsorption tower temperature control system of claim 1, wherein the first and second adsorption beds are disposed at the periphery of the inlet and outlet gas chambers, respectively, and the interstage gas chamber is disposed at the periphery of the first and second adsorption beds.
7. The active coke adsorption tower temperature control system of claim 2 or 3, further comprising a booster fan, wherein the booster fan is disposed on the second branch pipeline.
8. An active coke adsorption tower temperature control method, which is characterized in that the active coke adsorption tower temperature control method is carried out in the active coke adsorption tower temperature control system of any one of claims 1 to 7, and the active coke adsorption tower temperature control method comprises the following steps:
the active coke enters the tower from an active coke inlet at the top of the active coke adsorption tower, sequentially passes through the second-stage adsorption bed layer and the first-stage adsorption bed layer from top to bottom and is sent out from an active coke outlet at the bottom of the tower;
the flue gas to be purified enters an inlet gas chamber of the active coke adsorption tower through a flue gas feeding pipeline to be purified, and is in cross flow contact with active coke in a first-stage adsorption bed layer to perform first-stage adsorption purification, the flue gas which completes the first-stage adsorption purification is subjected to gas redistribution through an interstage gas chamber and then ascends to enter a second-stage adsorption bed layer to be in cross flow contact with the active coke to perform second-stage adsorption purification, the flue gas which completes the second-stage adsorption purification leaves the active coke adsorption tower from an outlet gas chamber, one part of the purified flue gas which leaves the active coke adsorption tower is sent to a chimney, and the other part of the purified flue gas is sent to the flue gas feeding pipeline to be purified and/or the.
9. The temperature control method for the activated coke adsorption tower as recited in claim 8, wherein the temperature of the flue gas to be purified is 160-280 ℃, and the inlet temperatures of the first-stage adsorption bed and the second-stage adsorption bed are 130-170 ℃ respectively.
10. The active coke adsorption tower temperature control method according to claim 8, wherein the mass ratio of the purified flue gas sent to the flue gas feeding line to be purified to the flue gas to be purified is 0-3; the mass ratio of the purified flue gas sent to the interstage air chamber to the flue gas at the outlet of the first-stage adsorption bed layer is 0-2.
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